Method and installation for controlling at least one cryogenic centrifugal compressor compression line

ABSTRACT

The inventive method consists in: 
 
selecting a pre-determined curve (C′ OPT ), 
 
which can be represented in the form of a first parameter (NU) that is representative of the speed of rotation of a compressor, according to a second parameter (X) that is representative of the mass flow of said compressor; regulating the speed of rotation of the downstream compressor according to the relative values of the instantaneous suction pressure of the upstream compressor and of a variable set pressure; and regulating the variable set pressure according to the instantaneous value (NU 4 (inst)), for the downstream compressor, of the parameter that is representative of the speed of rotation and the theoretical value (NU 4 (th)) of said first parameter, which is located on the pre-determined curve (C OPT ), which corresponds to the instantaneous value (X 4 (inst)) of the second parameter representative of the mass flow.

The present invention relates to a method and an installation for controlling at least one cryogenic centrifugal compressor, as well as a corresponding compression line and refrigeration installation.

The invention applies for example to the cooling of superconducting components of particle accelerators.

The pressures discussed here are absolute pressures.

The cooling of the superconducting components of particle accelerators requires the use of a fluid in equilibrium at low temperature and at low pressure, particularly helium, of which the vaporization provides the necessary heat transfers.

The refrigeration installations used in these applications comprise liquefaction units which, using helium gas at atmospheric pressure and ambient temperature, are able to supply liquid helium in equilibrium with its gas phase at temperatures of about 2K and at pressures of about 30 mbar.

The power dissipated by the superconducting components vaporizes helium, which must be recompressed in order to be recycled to the liquefaction unit, of which the inlet pressure is set at a value in the range of atmospheric pressure. The role of the compression line is to control its own inlet pressure and hence the liquid helium temperature.

At present, only compression lines with centrifugal compressors in series are suitable for compressing, at the desired compression ratio, a sufficient flow rate for obtaining medium or high refrigeration capacities. The centrifugal compressors are accordingly dimensioned to provide the desired compression ratio for the nominal mass flow rate of helium gas vaporized by the superconducting components operating at full capacity.

During startup, waiting periods, or the operation of the superconducting components at reduced capacity, the cooling requirements decrease, and this is accompanied by a commensurate reduction of the mass flow rate of helium gas vaporized and introduced into the compression line. This decrease in the mass flow rate is liable to cause stalling of the compressors, which must provide a constant compression ratio.

In the case of compressors operating at ambient temperature, the above problem is solved simply by adjusting the flow rate of each compressor. For this purpose, each compression stage is provided with a recycle line, which can be used to increase the mass flow rate of each compressor, and thereby to prevent its stalling.

However, this solution cannot be applied to cryogenic compressors mounted in series, because the solution whereby gas is recycled between each compression stage in order to adjust the operating point of each compressor would require intermediate coolings, would prove to be extremely complicated to implement, and would remove cooling capacity from the refrigerator.

Such cryogenic compressors are also subject to specific contingencies, which must be taken into account for their control.

Thus, given that this concerns a cryogenic system, the temperature of each of the compression stages is variable.

Furthermore, given that the flow treated by the compressors is sent to a refrigerator, the latter imposes a flow rate limitation, corresponding to the flow rate which it can accept.

Moreover, the control process is not time-dependent. In fact, the flow rate of gas to be treated results from the evaporation of a portion of liquid, for which the pressure is decreased, this flow rate being obtained by appropriately varying the suction pressure of the first compression stage.

Such a variation is linked to the various parameters of the liquid, on which the pumping is carried out, that is, in particular, the quantity, superheat state, or the residual power dissipated in this liquid.

Considering the above factors, it is an object of the invention to propose a method allowing the reliable control of at least one centrifugal cryogenic compressor, and which in particular makes it possible, at any time, to bring each compressor to a stable state, which can nonetheless be different from its nominal state.

For this purpose, one subject of the invention is a method for controlling a compression line comprising at least one cryogenic centrifugal compressor, said line being able in particular to compress a gas initially at low temperature and at low pressure, in particular helium, arriving from a vessel, method in which the speed of rotation of the or each compressor is controlled, characterized in that it comprises the following steps:

-   -   a predetermined curve is selected, which can be represented in         the form of a first parameter representative of the speed of         rotation of a compressor, as a function of a second parameter,         representative of the mass flow rate of said compressor;     -   the speed of rotation of the cryogenic centrifugal compressor         disposed furthest downstream of the compression line is         regulated as a function of the relative values, on the one hand,         of the instantaneous pressure at the inlet of the cryogenic         centrifugal compressor located furthest upstream of the         compression line and, on the other, of a variable pressure         setpoint; and     -   the variable pressure setpoint is regulated as a function of the         value of the ratio between, on the one hand, the instantaneous         value, for the downstream compressor, of the first parameter         representative of the speed of rotation of the compressor and,         on the other, the theoretical value of this first parameter,         situated on said predetermined curve, which corresponds to the         instantaneous value, for this downstream compressor, of the         second parameter representative of the mass flow rate.

According to other features of the invention:

-   -   the parameter representative of the speed of rotation is the         reduced-reduced speed.     -   the parameter representative of the mass flow rate is the         reduced-reduced flow rate.     -   in a representation which includes the compression ratio as a         function of the reduced-reduced flow rate, the predetermined         curve defines a second predetermined curve which is situated to         the right of a stalling curve of the compressor.     -   the second predetermined curve passes through the nominal         operating point.     -   for a given compression ratio, the distance between the second         predetermined curve and the stalling curve is proportional to         the value of the compression ratio.     -   the variable pressure setpoint is regulated by regulating an         attenuation coefficient, and by multiplying this attenuation         coefficient by a fixed value in order to obtain said variable         pressure setpoint.     -   the fixed value is equal to a desired pressure value at the         inlet of the upstream compressor, in particular 30 mbar.     -   the variable pressure setpoint is increased when the         instantaneous value, for the downstream compressor, of the         parameter representative of the speed of rotation, is less than         the theoretical value.     -   the speed of rotation of the downstream cryogenic centrifugal         compressor is increased when the instantaneous pressure at the         inlet of the upstream cryogenic centrifugal compressor is higher         than the variable pressure setpoint.     -   a downstream compressor is provided as well as at least one         other compressor and a speed of rotation is assigned to the or         to each other compressor, corresponding to the theoretical         value, for each other compressor, of the first parameter         representative of the speed of rotation, this value being         situated on the predetermined curve and corresponding to the         instantaneous value of the second parameter, representative of         the mass flow rate.     -   a downstream compressor is provided as well as at least one         other compressor and, at least during a startup phase of said         compressor, a speed of rotation is applied to the or to each         other downstream compressor, corresponding to the product of the         speed of rotation of the downstream compressor and a         predetermined coefficient.     -   after the or each cryogenic centrifugal compressor has reached         its nominal speed, energy is supplied, particularly electrical,         in the vessel, when the distance between an instantaneous         operating point and the stalling curve becomes less than a         preset minimum value.     -   a fraction of gas is recycled from downstream to upstream of the         compression line via a recycle line, the flow rate actually sent         downstream of this line, particularly to a liquefaction unit of         this gas, is measured, and the gas flow in the recycle line is         regulated as a function of the relative values, on the one hand,         of the flow rate actually sent downstream of the compression         line and, on the other, of a threshold flow rate, which         corresponds in particular to a flow rate that is acceptable as         regards this liquefaction unit.     -   auxiliary gas is injected at a temperature substantially higher         than that of the gas flowing in the compression line, in         particular at ambient temperature, and the injection of this         auxiliary gas is regulated as a function of the relative values,         on the one hand, of the gas flow rate downstream of the         compression line and, on the other, of a threshold flow rate,         corresponding in particular to a flow rate that is acceptable as         regards a liquefaction unit of this gas.

A further subject of the invention is an installation for controlling a compression line comprising at least one cryogenic centrifugal compressor, for the putting into practice of the method as described above, characterized in that it comprises:

-   -   first regulating means, able to regulate the speed of rotation         of the cryogenic centrifugal compressor located downstream of         the compression line, as a function of the relative values, on         the one hand, of the instantaneous pressure at the inlet of the         cryogenic centrifugal compressor situated upstream of the         compression line and, on the other, of a variable pressure         setpoint; and     -   second regulating means, able to regulate the variable pressure         setpoint as a function of the value of the ratio between, on the         one hand, the instantaneous value, for the downstream         compressor, of the first parameter of the predetermined curve,         representative of the speed of rotation of the compressor and,         on the other, the theoretical value of this first parameter,         situated on this predetermined curve, which corresponds to the         instantaneous value, for the downstream compressor, of the         second parameter of this predetermined curve, representative of         the mass flow rate of the compressor.

According to other features of the invention:

-   -   the speed regulating means comprise a first regulation loop         which has a setpoint equal to the variable pressure setpoint, a         measurement, equal to the pressure at the inlet of the upstream         cryogenic centrifugal compressor, and an output able to regulate         the speed of the downstream cryogenic centrifugal compressor.     -   the means for regulating the variable pressure setpoint comprise         a second regulation loop, having a setpoint equal to 1, a         measurement equal to the ratio between the instantaneous and         theoretical values of the first parameter, and an output able to         modify the value of this variable pressure setpoint.     -   the output of the second regulation loop terminates in a         multiplication module able to multiply the value of this output         by a fixed value.     -   this fixed value is equal to a pressure value desired at the         inlet of the upstream compressor, in particular 30 mbar.     -   the installation further comprises at least one computation         module able to calculate at any time, for the or for each         compressor, the instantaneous and theoretical values of the         first parameter, representative of the speed of rotation, and         the instantaneous value of the second parameter, representative         of the mass flow rate.     -   the installation comprises means able to supply energy,         particularly electrical, to the vessel, when the distance         between the operating point and the stalling curve becomes less         than a preset minimum value.     -   the installation comprises an energy regulating loop, having a         setpoint equal to said preset minimum value, a measurement         linked to another computation module, able to calculate, at any         time, the distance between the operating point and the stalling         curve, and an output linked to the energy supply means.     -   the installation comprises a recycle line, able to recycle a         fraction of gas from downstream to upstream of the compression         line, and flow regulating means, able to regulate the gas flow         in this recycle line as a function of the relative values, on         the one hand, of the flow rate actually sent downstream of the         compression line and, on the other, of a threshold flow rate.     -   the flow rate regulating means comprise a recycle flow         regulating loop having a setpoint equal to the threshold flow         rate, a measurement corresponding to the instantaneous value of         the rate of flow actually sent downstream of the compression         line, and an output linked with an open-shut member, in         particular a valve, with which the recycle line is equipped.     -   the installation comprises a line for injecting an auxiliary gas         at a temperature substantially higher than that of the gas         flowing in the compression line, in particular at ambient         temperature, and injection regulating means, able to regulate         the injection of this auxiliary gas as a function of the         relative values, on the one hand, of the flow rate of the gas         flowing downstream of the compression line and, on the other, of         a threshold flow rate.     -   the injection regulating means comprise an injection regulating         loop having a setpoint equal to the value of the threshold flow         rate, a measurement equal to the instantaneous value of the gas         flow rate flowing downstream of the compression line, and an         output linked with an open-shut member, in particular a valve,         with which the injection line is equipped.

A further subject of the invention is a compression line comprising at least one cryogenic centrifugal compressor, and an installation for controlling the or each compressor, characterized in that this control installation conforms to the above description.

A final subject of the invention is an installation for refrigeration by vaporization of a liquefied gas at low pressure and low temperature, particularly helium, comprising a vessel containing a two-phase fluid at low temperature and at low pressure, a unit for liquefaction of this gas, a feed line for two-phase fluid at low temperature and at low pressure, equipped with means for expanding this liquefied gas, connecting the liquefaction unit to the vessel, and a line for compressing the gas phase connecting the vessel to the liquefaction unit, characterized in that the compression line conforms to the above description.

The invention will be better understood from a reading of the description that follows, given only as a non-limiting example, and with reference to the drawings appended hereto, in which:

FIG. 1 is a schematic view, showing a train of cryogenic centrifugal compressors;

FIG. 2 is a graph showing the compression field of one of these cryogenic centrifugal compressors;

FIG. 3 is a graph showing an optimal behavior, in the sense of the invention, of a cryogenic centrifugal compressor;

FIG. 4 is a schematic view showing an installation, according to the invention, for controlling the train of compressors shown in FIG. 1;

FIGS. 5 to 8 are schematic views similar to those of FIG. 4, showing embodiments of the control installation according to the invention; and

FIG. 9 is a schematic view, similar to FIG. 1 showing an additional embodiment of the invention.

FIG. 1 shows an installation for refrigeration by liquid helium, used for example for cooling superconducting components of particle accelerators.

This installation comprises a helium liquefaction unit 1, or refrigerator, comprising compressors, heat exchangers and expansion means, not shown. Also provided is a first vessel 3 for storing liquid helium in equilibrium with its gas phase, and a second vessel 5 for storing liquid helium in equilibrium with its gas phase, which provides the heat exchanges with the component E to be refrigerated.

The helium liquefaction unit 1, after expansion in a pressure reducing valve 7, delivers liquid helium in equilibrium with its gas phase to the first vessel 3. In operation, the helium is then at a temperature of about 4.4 K and at a pressure of about 1.2 bar.

The liquid of the first vessel 3 is extracted via a line 9, cooled in a heat exchanger 11, then expanded in a pressure reducing valve 13 before being introduced in equilibrium with its gas phase into the second vessel 5. In operation, the helium in this vessel must be at a temperature of about 2K and at a pressure of about 31.3 (mbar) (or hPa).

The gas overhead of the second vessel 5 is aspirated, after countercurrent heating in the heat exchanger 11, into a compression line 15 which returns the helium gas into the liquefaction unit 1.

The discharge pressure of the compression line is in imposed by the liquefaction unit 1 at a value of about 1.15 bar. In operation, the compression line is able to lower the equilibrium pressure and hence the equilibrium temperature of the helium in the second vessel 5 to the desired value.

Such a refrigeration installation is described in documents FR-A-2 679 635 and U.S. Pat. No. 5,499,505.

The compression line shown in FIG. 1 comprises four cryogenic centrifugal compressors mounted in series, which are assigned the numerals CCC₁ to CCC₄.

The following parameters will be used for an easier description of the operation of the compressors:

-   -   “reduced” flow rate of a compressor: Y=D×{square root}{square         root over (T)}/P     -   “reduced” speed of a compressor; n=N/{square root}{square root         over (T)}     -   where D is the mass flow rate through the compressor, T the         compressor inlet temperature, P the compressor inlet pressure         and N the compressor speed of rotation,     -   “reduced-reduced”, or, “reduced-normed” flow rate of a         compressor; X═Y/Y_(N)     -   and “reduced-reduced”, or “reduced-normed” speed of a         compressor; NU=n/n_(N)     -   where Y_(N) is the nominal “reduced” flow rate of the         compressor, that is in operating conditions corresponding to         those of its design, and n_(N) is the nominal “reduced” speed of         the compressor, that is in operating conditions corresponding to         those of its design.

The graph in FIG. 2 shows the compression field of a centrifugal compressor in a “reduced-reduced” flow rate/compression ratio plane.

The curve C_(DEC) of stalling in the impeller vanes, shown by solid lines, divides the compression field of the compressor into a stable operating zone to the right of the stalling curve, and an unstable operating zone to the left of the stalling curve.

Thanks to the use of “reduced-reduced” variables, this curve C_(DEC) makes it possible to analyze the operation of a compressor in conditions other than those defined for the nominal speed, and also to compare the operation of different compressors, which do not necessarily have identical fields.

By reference to the graph in FIG. 2, an optimal path is defined, which each compressor is presumed to follow, thanks to the control method of the invention.

This optimal path C_(OPT), which is shown by dotted lines, is situated to the right of the stalling curve. It passes through the point (Taux_(nom); 1), symbolized by a circle which corresponds to a nominal operating point, for example defined by the operator.

This optimal path is the locus, passing through the above point (Taux_(nom); 1) of the operating points situated at a “similar” or “proportional” distance from the stalling curve. This means that the distance between the operating point of the compressor and the stalling curve, which is proportional to the compression ratio, is defined by the same ratio (X−X_(s))/X_(s) on the field of each compressor, this ratio also being called the distance coefficient.

Under these conditions, since the sensitivity to stalling increases with the compression ratio, the distance between the stalling curve and the optimal path at constant compression ratio is defined as follows: ((X−X_(s))/X_(s))×(Taux/Taux_(Nom)).

This distance varies from 0 for a compression ratio of 1, to its maximum value d_(NOM), corresponding to the nominal compression ratio Taux_(NOM). By referring to FIG. 2, it is thus equal to d₁=(X₁−X_(s)/X_(s))×(Taux₁/Taux_(NOM)) and to d₂=(X₂−X_(s)/X_(s))×(Taux₂/Taux_(NOM)), for given respective points X₁ and X₂.

As shown in FIG. 3, the optimal path C_(OPT) of FIG. 2 can be shown in the form of another graph. On this graph, the reduced-reduced flow rate X is plotted on the x-axis, while the reduced-reduced speed NU is plotted on the y-axis.

This optimal path C′_(OPT), in its form NU=f(X) varies from the point (0; 0) corresponding to a compressor at rest, to the point (1; 1) which corresponds to the nominal operation of this compressor.

FIG. 4 shows an installation for controlling the train of centrifugal cryogenic compressors shown in FIG. 1.

This installation comprises a pressure regulation loop BRP. This loop receives, via the line m₁, the measurement of the suction pressure of the first cryogenic compressor CCC₁.

Moreover, the setpoint applied to this regulation loop, which is symbolized by the line c₁, is described in greater detail below. Finally, the output s₁ of this loop BRP is linked to the downstream compressor CCC₁, in order to vary its speed of rotation.

A speed regulation loop BRV is also provided. Three lines, assigned respectively the numerals m₂, c₂ and s₂, represent the measurement, the setpoint, and the output of this second regulation loop.

The installation further comprises four computation modules MC₁, MC₂, MC₃ and MC₄, each of which is connected to a corresponding compressor CCC₁ to CCC₄.

The module MC₁ is connected to sensors of the inlet pressure P₁ and of the inlet temperature T₁ of the compressor C₁, via a line L₁. Similarly, the modules MC₂, MC₃ and MC₄ are connected to sensors of the inlet pressure P₂ to P₄ and the inlet temperature T₂ to T₄ of the compressors CCC₂ to CCC₄, via lines L₂ to L₄.

A sensor of the mass flow rate D of gas flowing in the compression line is connected to each of the computation modules MC₁ to MC₄, via a line LD. These various computation modules each comprise computation and data storage means.

The module MC₄ calculates the coordinates X₄ (inst) and NU₄(inst) at any time, from the values measured by the various associated sensors, relative to the flow rate, the temperature and the pressure.

The module MC₄ also calculates, for this given X₄ (inst), the theoretical value NU₄ (th), situated on the optimal path C′_(OPT) in FIG. 3.

The values of X₄ (inst), NU₄ (inst) and NU₄ (th) are plotted in FIG. 3.

The module MC₄ also calculates the ratio NU₄(inst)/NU₄(th), then sends the corresponding result to the regulation loop BRV, via the line m₂.

Furthermore, the regulation loop BRV compares this measurement m₂ to the setpoint c₂, which is in this case equal to 1. The value of the output s₂, which constitutes an attenuation coefficient, is then adjusted accordingly.

This output s₂ is sent to an additional computation module mc₄, which performs the multiplication between this attenuation coefficient s₂ and a fixed pressure setpoint, symbolized by the line cp. This fixed setpoint corresponds to the target pressure upstream of the first compressor CCC₁, that is for example 30 mbar.

The product s₂*cp thus obtained constitutes the setpoint c₁ of the pressure regulation loop BRP. It is accordingly important to note that this setpoint c₁ is variable, or “floating”.

Furthermore, each of the computation modules MC₁ to MC₃ calculates the coordinates of the points (X_(i) (inst); NU_(i)(inst)) at any time, i varying from 1 to 3, for each compressor CCC₁ to CCC₃. In a similar manner as described above for MC₄, these modules calculate the values of NU_(i)(th), which correspond to the values of NU situated on the optimal path, for each of the X_(i)(inst).

The control of the train of compressors in FIG. 1 will now be explained, with reference to FIGS. 3 and 4.

It is assumed that, at any given time, the coordinates of the operating point of the downstream compressor CCC₄ are (X₄(inst); NU₄(inst)), as shown on the graph in FIG. 3.

Under these conditions, NU₄(inst) is lower than NU₄(th), situated on the optimal path C′_(OPT). In consequence, the ratio NU₄ (inst)/NU₄ (th), which constitutes the measurement m₂, is less than 1.

This measurement m₂ of the speed regulation loop BRV is hence lower than its setpoint c₂, which is equal to 1, so that the output signal s₂ is increased. This tends to increase the value of the setpoint c₁ of the pressure regulation loop BRP.

The speed of rotation N₄ of the compressor CCC₄ is then increased commensurately, via the output signal s₁. The volumetric flow rate of gas created by this compressor CCC₄ is also increased, together with its compression ratio.

This is accordingly accompanied by a commensurate decrease in the suction pressure P₄ of the downstream compressor CCC₄, accompanied by an increase in the discharge gas temperature.

Finally, the value of the reduced-reduced flow rate X₄ increases. This increase in the reduced-reduced flow rate, and that of the reduced-reduced speed NU₄, is symbolized on the graph in FIG. 3 by the next operating point (X′₄(inst);NU′₄(inst)), situated to the top right of the preceding operating point (X₄(inst) NU₄(inst)), that is closer to the optimal path.

Since the various regulation loops BRP and BRV act continuously, the curve x4=f(NU₄) progressively approaches the optimal path C′_(opt), greeting it at a point (X″₄; NU″₄), shown in FIG. 3.

When the operating curve meets the optimal path, the measured value of NU₄ and the theoretical value of NU₄ become equal, so that the speed regulation loop BRV is deactivated. The setpoint c₁ of the pressure regulation loop BRP is hence maintained at a constant value.

Furthermore, if the measurement m₁ of this loop, that is the suction pressure P₁ of the compressor CCC₁, does not vary, the mass flow rate treated by the compressor decreases, as well as the reduced-reduced flow rate X₄. Thus, the curve NU₄=f (X₄) meets the operating point (1; 1), substantially along a thicker portion of the curve, situated at the upper portion of the optimal path C′_(OPT) in FIG. 3.

This means that the speed of rotation of the compressor C₄ will increase until it reaches the nominal speed, which corresponds to a pressure P₁ of 30 mbar. This makes it necessary to perform a speed adjustment, for these nominal conditions, which is explained below.

We shall now return to the action of the regulation loops BRV and BRP, on the upstream compressors CCC₁ to CCC₃.

We have shown that, on the one hand, the downstream compressor CCC₄ defines, at any time, the mass flow rate which enables it to operate satisfactorily.

We have also shown that the computation modules MC₁, MC₂ and MC₃ calculate at any time, the values of NU making it possible to locate on the optimal path C′_(OPT) for each compressor. In this case, these values are NU₁(th), NU₂(th) and NU₃(th).

Under these conditions, each computation module MC₁ to MC₃ controls a corresponding compressor CCC₁ to CCC₃, assigning to it the speeds N₁(th) to N₃(th) which correspond to the theoretical values of NU presented immediately above. This is achieved via the control lines LC₁ to LC₃.

FIG. 5 shows a variant of the installation in FIG. 4. This variant comprises all the elements in FIG. 4, as well as additional means pertaining to the control of the upstream compressors CCC₁ to CCC₃.

In this FIG. 5, the computation modules MC₁ to MC₃ receive, in a similar manner as described above, data enabling them to calculate the instantaneous values of X₁ to X₃, as well as the respective instantaneous and theoretical values of NU₁ to NU₃.

An additional control line LS is also provided, connecting the output of the pressure regulation loop BRP to each of the computation modules MC₁ to MC₃. This line LS is provided with branch connections ld₁ to ld₄, each of which is sent to a corresponding multiplication module M₁ to M₃.

Each module M₁ to M₃ performs the multiplication, by a given coefficient a₁, a₂, or a₃, of the signal transmitted via the line LS, that is the speed of rotation N₄ which is applied to the downstream compressor CCC₄. Under these conditions, the lines ld′₁ to ld′₃, situated downstream of the modules M₁ to M₃ transmit signals representative of the products (N₄*a₁), (N₄×a₂) and (N₄×a₃).

Furthermore, lines LS′₁ to LS′₃ issue from each computation module MC₁ to MC₃. These lines transmit the following products, for i=1 to 3: N₁(th)/(a_(i)×N₄).

As explained above, the values of N_(i)(th) are situated on the optimal path in FIG. 3.

The lines ld₁ to ld₃, as well as LS′₁ to LS′₃, terminate in pairs in additional multiplication modules M′₁ to M′₃. Each of these modules carries out the multiplication between the data transmitted via the different lines, or, for i=1 to 3: (N₄×a_(i))×N_(i)(th)/N₄×a_(i).

The corresponding product, which is equal to N_(i) (th), is then sent to the compressors C₁ to C₃, via the respective control lines LC′₁ to LC′₃.

The use of these various multiplication modules M₁ to M₃, and of M′₁ to M′₃, is advantageous in the sense that the times for computation of the adjustment by the modules MC₁, MC₂ and MC₃, which can be long depending on the speed of the central processor, accordingly have a reduced effect on the quality of control.

FIG. 6 shows a variant of FIG. 5. This variant comprises all the means in FIG. 5, as well as additional means corresponding to the operation of the compressors under nominal conditions.

When the pressure P₁ reaches the target value, for example 30 mbar as shown above, the speeds of the various compressors tend towards fixed values.

In consequence, in the absence of additional measurement, the mass flow rate of gas transported by the compressors is reduced, so that the operating points tend to approach the stalling curve C_(DEC), shown in FIG. 2.

Furthermore, it is inconceivable to accelerate the various compressors. In fact, if this were the case, the pressure P₁ would fall below the above objective value.

The solution to this problem is provided by the installation in FIG. 6.

FIG. 6 shows an energy regulation loop BRE, of which the measurement m₃ line arrives from a computation module MCD. This module permanently calculates the distance between the instantaneous operating point and the stalling curve, for any of the compressors of the train, for example, as shown, the compressor CCC₁.

By again referring to FIG. 2, this instantaneous distance d(inst) corresponds to the value: ((X(inst)−Xs)/Xs)×(Taux(inst)/Taux_(NOM).)

Furthermore, the setpoint c₃ of the loop BRE corresponds to a minimum, or so-called safety distance, above which any operating point must be situated. This minimum distance, symbolized by reference d_(MIN) in FIG. 2, is for example equal to 50% of the distance between the stalling curve C_(DEC) and the optimal path C_(OPT).

Finally, the output S₃ of the regulation loop BRE is sent to an electrical energy supply means disposed in the bath 5. This is for example a resistor R, with the understanding that any means for supplying energy, other than electrical, can be considered.

In service, when the operating point of the compressor CCC₁ approaches too close to the stalling curve C_(DEC), the regulation loop BRE injects power into the helium bath 5. This causes the vaporization of a commensurate quantity of helium, making it possible to increase the mass flow rate of gas flowing in the compressors, thereby guaranteeing that the operating point deviates from the stalling curve.

FIG. 7 shows a variant of FIG. 6, relative to the gas pressure reducing phase.

During such a pressure reduction, the compressors treat a maximum flow rate of gas, which is higher than the value of the nominal flow rate. Under these conditions, such a flow rate is sometimes higher than a limit value acceptable as regards the refrigerator 1, to which this helium gas is sent.

As shown in FIG. 7, a recycle line LR is provided, provided with a valve V which extends from downstream of the compressor CCC₄ to upstream of the compressor CCC₁. A computation module MCR receives, via the respective lines LD′ to LR′, data relative, on the one hand, to the flow rate D of gas flowing immediately downstream of the compressor CCC₄ and, on the other, the recycle rate DR flowing through the line LR.

This computation module MCR transmits a signal representative of the difference between the two flow rates, which corresponds to the flow rate sent to the refrigerator, via a line m_(R) to an additional regulation loop, assigned the numeral BRR.

The setpoint C_(R) of this regulation loop corresponds to the maximum flow rate that the refrigerator can accept. Finally, the output SR Of this loop BRR can be used to control the recycle valve V.

In service, when the flow rate sent to the refrigerator, which is equal to the difference (D−D_(R)) between the outlet flow rate from CCC₄ and the possible recycle rate, reaches the maximum value c_(R), the regulation loop BRR actuates the opening of the valve V. This makes it possible to increase the recycle rate, and hence to reduce the flow rate actually sent to the refrigerator, in order to guarantee the integrity of the latter.

It should be observed that this recycle operation tends to increase the reduced-reduced flow rate in two ways. In fact, this recycling causes an increase, not only of the mass flow rate, but also of the temperature of the gas sent to the unit 1, since gas at a higher temperature is recycled.

FIG. 8 shows an embodiment of the installation in FIG. 7.

In the installation in this FIG. 8, the recycle line is replaced by a line LA, conveying gas at ambient temperature, for example close to 300 K. Under these conditions, the measurement m′_(R) of the regulation loop BRR′ corresponds to the flow rate of gas flowing downstream of the compressor CCC₄.

In service, when this measured flow rate reaches the setpoint value c′_(R), which still corresponds to the maximum flow rate accepted by the refrigerator, the loop BRR′ actuates the opening of the recycle valve V′, via the output s′R, thereby causing the injection of gas upstream of the compressor CCC₁.

This injection of gas at ambient temperature causes an increase in the temperature of the resulting mixture. This causes an increase in the reduced-reduced flow rate X, making it possible to deviate the operating points from the stalling curves, while maintaining the flow rate at an acceptable value as regards the refrigerator.

FIG. 9 shows another embodiment of the invention.

The compression therein is performed in a composite manner, by combining three compressors CCC₁ to CCC₃ operating at cryogenic temperature, as well as a compressor CCA, operating at ambient temperature. It must be understood that the number of compressors operating at cryogenic temperature or at ambient temperature can be chosen at random, as a variant.

Under these conditions, only the cryogenic compressors CCC are controlled in a manner according to the invention.

The invention is not limited to the examples described and shown.

Thus, the method of the invention can also be applied for the control of a single compressor.

In this eventuality, the measurement m₁ of the pressure regulation loop BRP corresponds to the suction pressure of this single compressor.

Furthermore, the control process explained above also applies to a startup phase, both of a train of compressors and of a single compressor.

Finally, the optimal path may be different from the one shown in FIG. 2. In particular, the distance between this optimal path and the stalling curve may not be proportional to the value of the compression ratio. 

1-29. (canceled)
 30. A method for controlling a compression line comprising at least one cryogenic centrifugal compressor, said line being able in particular to compress a gas initially at low temperature and at low pressure, in particular helium, arriving from a vessel, method in which the speed of rotation of the or each compressor is controlled, wherein it comprises the following steps: a) a predetermined curve is selected, which can be represented in the form of a first parameter representative of the speed of rotation of a compressor, as a function of a second parameter, representative of the mass flow rate of said compressor; b) the speed of rotation of the cryogenic centrifugal compressor disposed furthest downstream of the compression line is regulated as a function of the relative values, on the one hand, of the instantaneous pressure (P₁) at the inlet of the cryogenic centrifugal compressor (CCC₁) located furthest upstream of the compression line and, on the other, of a variable pressure setpoint (c₁); and c) the variable pressure setpoint (c₁) is regulated as a function of the value of the ratio between, on the one hand, the instantaneous value (NU₄(inst)), for the downstream compressor (CCC₄), of the first parameter representative of the speed of rotation of the compressor and, on the other, the theoretical value (NU₄(th)) of this first parameter, situated on said predetermined curve (C′_(OPT)), which corresponds to the instantaneous value (X₄(inst)), for this downstream compressor (CCC₄), of the second parameter representative of the mass flow rate.
 31. The method of claim 30, wherein the parameter representative of the speed of rotation is the reduced-reduced speed (NU).
 32. The method of claim 30, wherein the parameter representative of the mass flow rate is the reduced-reduced flow rate (X).
 33. The method of claim 30, wherein, in a representation which includes the compression ratio (TAUX) as a function of the reduced-reduced flow rate (X), the predetermined curve defines a second predetermined curve (C_(OPT)) which is situated to the right of a stalling curve (C_(DEC)) of the compressor.
 34. The method of claim 33, wherein said second predetermined curve (C_(OPT)) passes through the nominal operating point (1; TAUX_(NOM)).
 35. The method of claim 33, wherein, for a given compression ratio, the distance (d) between the second predetermined curve (C_(OPT)) and the stalling curve (C_(DEC)) is proportional to the value of the compression ratio (TAUX).
 36. The method of claim 30, wherein the variable pressure setpoint (c₁) is regulated by regulating an attenuation coefficient (s₂), and by multiplying this attenuation coefficient by a fixed value (cp) in order to obtain said variable pressure setpoint.
 37. The method of claim 36, wherein the fixed value (cp) is equal to a desired pressure value at the inlet of the upstream compressor (CCC₁), in particular 30 mbar.
 38. The method of claim 30, wherein the variable pressure setpoint (c₁) is increased when the instantaneous value (NU₄(inst)), for the downstream compressor (CCC₄), of the parameter representative of the speed of rotation, is less than the theoretical value (Nu₄(th)).
 39. The method of claim 30, wherein the speed of rotation (N₄) of the downstream cryogenic centrifugal compressor (CCC₄) is increased when the instantaneous pressure (P₁) at the inlet of the upstream cryogenic centrifugal compressor (CCC₁) is higher than the variable pressure setpoint (c₁).
 40. The method of claim 30, wherein a downstream compressor (CCC₄) is provided as well as at least one other compressor (CCC₁ to CCC₃) and in that a speed of rotation is assigned to the or to each other compressor (CCC₁ to CCC₃), corresponding to the theoretical value (NU₁(th) to NU₃(th)), for each other compressor, of the first parameter representative of the speed of rotation, this value being situated on the predetermined curve (C′_(opt)) and corresponding to the instantaneous value (X₁(inst) to X₃(inst)) of the second parameter, representative of the mass flow rate.
 41. The method of claim 30, wherein a downstream compressor (CCC₄) is provided as well as at least one other compressor (CCC₁ to CCC₃) and in that, at least during a startup phase of said compressor, a speed of rotation (N₁ to N₃) is applied to the or to each other downstream compressor (CCC₁ to CCC₃), corresponding to the product of the speed of rotation (N₄) of the downstream compressor (CCC₄) and a predetermined coefficient (a₁ to a₃).
 42. The method of claim 30, wherein, after the or each cryogenic centrifugal compressor has reached its nominal speed (FIG. 6), energy is supplied, particularly electrical, in the vessel (5), when the distance (d_(inst)) between an instantaneous operating point (X_(inst); TAUX_(inst)) and the stalling curve (C_(DEC)) becomes less than a preset minimum value (d_(MIN)).
 43. The method of claim 30, wherein a fraction of gas is recycled from downstream to upstream of the compression line via a recycle line (LR), the flow rate actually sent downstream of this line, particularly to a liquefaction unit (1) of this gas, is measured, and the gas flow in the recycle line is regulated as a function of the relative values, on the one hand, of the flow rate (m_(R)) actually sent downstream of the compression line and, on the other, of a threshold flow rate (C_(R)), which corresponds in particular to a flow rate that is acceptable as regards this liquefaction unit.
 44. The method of claim 30, wherein auxiliary gas (LA) is injected at a temperature substantially higher than that of the gas flowing in the compression line, in particular at ambient temperature, and in that the injection of this auxiliary gas is regulated as a function of the relative values, on the one hand, of the gas flow rate (m′_(R)) flowing downstream of the compression line and, on the other, of a threshold flow rate (C′_(R)), corresponding in particular to a flow rate that is acceptable as regards a liquefaction unit (1) of this gas.
 45. An installation for controlling a compression line comprising at least one cryogenic centrifugal compressor (CCC₁, CCC₂, CCC₃, CCC₄), for the putting into practice of the method of any one of the preceding claims, wherein it comprises: a) first regulating means (BRV), able to regulate the speed of rotation (N₄) of the cryogenic centrifugal compressor (CCC₄) located downstream of the compression line, as a function of the relative values, on the one hand, of the instantaneous pressure (P₁) at the inlet of the cryogenic centrifugal compressor (CCC₁) situated upstream of the compression line and, on the other, at a variable pressure setpoint (C₁); and b) second regulating means (BRP), able to regulate the variable pressure setpoint (c₁) as a function of the value of the ratio between, on the one hand, the instantaneous value (NU₄(inst)), for the downstream compressor (CCC₄), of the first parameter of the predetermined curve (C′_(OPT)), representative of the speed of rotation of the compressor and, on the other, the theoretical value (NU₄(th)) of this first parameter, situated on this predetermined curve, which corresponds to the instantaneous value (X₄(inst)), for the downstream compressor (CCC₄), of the second parameter of this predetermined curve, representative of the mass flow rate of the compressor.
 46. The installation of claim 45, wherein the speed regulating means comprise a first regulation loop (BRV) which has a setpoint (c₁) equal to the variable pressure setpoint, a measurement (m₁), equal to the pressure (P₁) at the inlet of the upstream cryogenic centrifugal compressor (CCC₁), and an output (s₁) able to regulate the speed of the downstream cryogenic centrifugal compressor (CCC₄).
 47. The installation of claim 45, wherein the means for regulating the variable pressure setpoint comprise a second regulation loop (BRP), having a setpoint (c₂) equal to one, a measurement (m₂) equal to the ratio between the instantaneous (NU₄(inst)) and theoretical (NU₄(th)) values of the first parameter, and an output (s₂) able to modify the value of this variable pressure setpoint.
 48. The installation of claim 47, wherein the output (s₂) of the second regulation loop (BRP) terminates in a multiplication module (mc₄) able to multiply the value of this output (s₂) by a fixed value (cp).
 49. The installation of claim 48, wherein this fixed value (cp) is equal to a pressure value desired at the inlet of the upstream compressor (CCC₁), in particular 30 mbar.
 50. The installation of claim 45, wherein it further comprises at least one computation module (MC₁ to MC₃) able to calculate at any time, for the or for each compressor, the instantaneous (NU(inst)) and theoretical (NU(th)) values of the first parameter, representative of the speed of rotation, and the instantaneous value (X(inst)) of the second parameter, representative of the mass flow rate.
 51. The installation of claim 45, for putting into practice the method of claim 42, wherein it comprises means (R) able to supply energy, particularly electrical, to the vessel (5), when the distance (d_(inst)) between the operating point (X_(inst), TAUX_(inst)) and the stalling curve becomes less than a preset minimum value (d_(MIN)).
 52. The installation of claim 51, wherein it comprises an energy regulating loop (BRE), having a setpoint (C₃) equal to said preset minimum value (d_(MIN)), a measurement (m₃) linked to another computation module (MCD), able to calculate, at any time, the distance (d_(inst)) between the operating point and the stalling curve, and an output (s₃) linked to the energy supply means (R).
 53. The installation of claim 45, for setting up the method of claim 14, wherein it comprises a recycle line (LR), able to recycle a fraction of gas from downstream to upstream of the compression line, and flow regulating means (BRR), able to regulate the gas flow in this recycle line as a function of the relative values, on the one hand, of the flow rate (m_(R)) actually sent downstream of the compression line and, on the other, of a threshold flow rate (c_(R)).
 54. The installation of claim 53, wherein the flow regulating means comprise a recycle flow regulating loop (BRR) having a setpoint (CR) equal to the threshold flow rate, a measurement (m_(R)) corresponding to the instantaneous value of the rate of flow actually sent downstream of the compression line, and an output (s_(R)) linked with an open-shut member, in particular a valve (V), with which the recycle line (LR) is equipped.
 55. The installation of claim 45, for putting into practice the method of claim 44, wherein it comprises a line (LA) for injecting an auxiliary gas at a temperature substantially higher than that of the gas flowing in the compression line, in particular at ambient temperature, and injection regulating means (BRR′), able to regulate the injection of this auxiliary gas as a function of the relative values, on the one hand, of the flow rate (m′_(R)) of the gas flowing downstream of the compression line and, on the other, of a threshold flow rate (C′_(R)).
 56. The installation of claim 55, wherein the injection regulating means comprise an injection regulating loop (BRR′) having a setpoint (C′_(R)) equal to the value of the threshold flow rate, a measurement (m′_(R)) equal to the instantaneous value of the gas flow rate flowing downstream of the compression line, and an output (s′_(R)) linked with an open-shut member, in particular a valve (V′), with which the injection line (LA) is equipped.
 57. A compression line comprising at least one cryogenic centrifugal compressor (CCC₁ to CCC₄), and an installation for controlling the or each compressor, wherein this control installation conforms to claim
 45. 58. An installation for refrigeration by vaporization of a liquefied gas at low pressure and low temperature, particularly helium, comprising a vessel (5) containing the two-phase fluid at low temperature and at low pressure, a unit (1) for liquefaction of this gas, a feed line for two-phase fluid at low temperature and at low pressure, equipped with means (7, 13) for expanding this liquefied gas, connecting the liquefaction unit to the vessel, and a line (15) for compressing the gas phase connecting the vessel to the liquefaction unit, wherein the compression line (15) conforms to claim
 57. 